Process for manufacturing gasoline additives of non-ester polyoxyalkylene amide

ABSTRACT

A process for preparing amide alkoxylates. More specifically, the invention provides a butoxylation process for producing poly(oxyalkylene) amides and poly(oxyalkylene) esters via an exchange reaction of (trans-amidation/trans-esterification) and involving removal of the poly(oxyalkylene) esters in the product mixtures so that a better performance products can be obtained. The invention further relates to the use of these compounds as fuel additives to decrease intake valve deposits, positively affecting the engine&#39;s octane requirement, control the increase of combustion chamber deposits and improve fuel quality. The invention further discloses a composition used as engine fuel, characterized in that it contains said poly(oxyalkylene)amide as the fuel additive.

FIELD OF INVENTION

[0001] This invention relates to a method of a gasoline additives producing and more particular to a process for manufacturing gasoline additives of non-ester polyoxyalkylene amide which is advantageous for decreasing intake valve deposits

decreasing octane requirement

controlling the additions of internal combustion chamber deposits and improving the fuel quantity.

BACKGROUND OF THE INVENTION

[0002] Many additives are known which can be added to gasoline additives to prevent or reduce deposit formation, e.g., polymeric surfactants as gasoline additives J. Chin. Colloid & Interface Soc., Vol. 19, No. 3, 1996, the recently publication as follows:

[0003] 1. Polyoxyalkylene Amide Composition

[0004] U.S. Pat. No. 5,352,251 (Oct. 4, 1994) of Shell Oil Company mentioned ring polyoxyalkylene amide as gasoline additives.

[0005] U.S. Pat. No. 5,693,107 (Dec. 2, 1997) of Shell Oil Company disclosed hydantoin polyoxyalkylene amide as gasoline additives.

[0006] U.S. Pat. No. 5,492,546 (Feb. 20, 1996) of Shell Oil Company disclosed a fuel composition.

[0007] U.S. Pat. No. 5,507,843 (1996) of Shell Oil Company disclosed a fuel composition.

[0008] U.S. Pat. No. 5,489,315 (1996) of Shell Oil Company disclosed a hydantoin polyether polyol as gasoline additives.

[0009] U.S. Pat. No. 5,458,661 (1995) of Shell Oil Company disclosed a fuel composition.

[0010] U.S. Pat. No. 5,458,660 (1995) of Shell Oil Company disclosed a fuel composition.

[0011] 2. Polyoxyalkylene Amines

[0012] U.S. Pat. No. 5,057,122 (Oct. 15, 1991) of Mobil Oil Company disclosed a diisocyanate derivatives composition as fuel additives and lubricants.

[0013] Other documents includes U.S. Pat. No. 4,604,103 (1986) of Chevron, U.S. Pat. No. 5,112,364 (1992) of BASF, U.S. Pat. Nos. 5,286,266 & 5,286,267 (1994) of Texaco, U.S. Pat. Nos. 5,286,478 (1993) & 5,203,879 (1993) & 4,810,261 (1989) & 4,747,851 (1988) of Texaco.

[0014] 3. Polyoxyalylene Amine Carbamates

[0015] U.S. Pat. No. 5,321,460 (1994) of Chevron disclosed linear propylene oxide of polyoxyalylene amine carbamates as a fuel composition. And includes U.S. Pat. Nos. 5,322,539 (1994), 5,321,460 (1994), 5,192,335 (1993) of Chevron, U.S. Pat. No. 423,321 (1980) of Chevron, U.S. Pat. No. 5,103,041 (1992) of B. P. (Phosgene Substitute Process), U.S. Pat. No. 4,568,358 (1986) of Chevron.

[0016] 4. Others

[0017] U.S. Pat. No. 5,296,003 (Mar. 22, 1994) of Chevron, U.S. Pat. No. 5,298,039 (Mar. 29, 1994) of BASF disclosed gasoline fuel comprised a nitro-detergent and polyester as a carried oil compound, wherein polyester compound starter is dialkyl phenol.

[0018] U.S. Pat. No. 5,246,006 (1993) of Exxon and U.S. Pat. No. 5,089,029 (1992) of Kao Corporation mentioned acrylonitrile reacted to guerbet alkyletheramino by addition process and reducing process.

[0019] The above-mentioned manufacturing polyoxyalkylene amide methods could produce a ester functional group compound, as follows:

[0020] The performance of engine was damaged by said compound which must remove, the high temperature combustion process leaded to add deposits and effect octane number.

SUMMARY OF THE INVENTION

[0021] It is an object of the present invention to provide a process for manufacturing gasoline additives of non-ester polyoxyalkylene amide which is advantageous for decreasing intake valve deposits and octane requirement.

[0022] It is another object of the present invention to provide a process for manufacturing gasoline additives of non-ester polyoxyalkylene controlling the combustion deposit additions and improving the fuel quantity.

[0023] The present invention is directed to manufacturing gasoline additives of non-ester polyoxyalkylene amide comprising three steps, referring to FIG. 1., there is shown a formula of reaction view of this invention. As follows three continue steps:

[0024] a. taking ethyl acetate for low-molecular weight of amino group reacted to amide group by amidation;

[0025] b. taking amide group as starter and 1,2-cycleoxide butane reacted to polyoxyalkylene amide and 1,2-cycleoxide-ether-amine-ester-amide by opening cycle polymeric etherealization; and

[0026] c. Using 1,2-epoxybutane-ether-amine-ester-amide reacted to 1,2-epoxybutane-amine-ether-amide by selective hydrolyze, and was removed acetic acid by-product by selective hydrolysis in sit.

[0027] In step(b), the product appeared other compounds by accident, as follows:

[0028] Those compounds poof is damaged engine by engine test which should be clean. Therefore, in step (c) was removed said compounds by selective hydrolyze and get non-ester polyoxyalkylene amide as follows:

[0029] The hydrolyze need specific conditions. The amidation made EDTA-triamide-BO bond of amide group which is selective hydrolyze ester functional group. The process included about 8 to 12% HCl, excellent is 10%, at 90 to 100° C. by refluxing and heating. When the controlling process was disappeared C═O absorption peak (1735 cm⁻¹) by IR analysis in short-term, the process is complete. The poly(1,2-epoxybutane)ether amide transformed poly(1,2-epoxybutane)ether amine. After hydrolyze, the poly(1,2-epoxybutane)ether amine composition showed a narrow Mw distribution, as follow the formula:

[0030] The tests of intake valve coking simulator (IVCS)

and thermal decomposition test and octane requirement reduction (ORR) for all yields showed excellent result which is non-ester functional group.

[0031] The above and other objects, features and advantages of the present invention will become apparent from the following detailed description taken with the accompanying drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

[0032]FIG. 1 is formula diagram of a preferred embodiment of the invention

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS EXAMPLES

[0033] Experimental procedures for the synthesis of ester-free poly(oxyalkylene)-amide gasoline additives

Example 1

[0034] Preparation of Triamide from Diethylenetriamine (DETA) and Ethyl Acetate

[0035] 1. A mixture of DETA (35.20 g, 0.34 moles) and ethyl acetate (176 g) were charged into a one-liter autoclave.

[0036] 2. The autoclave was sealed and was purged off air by pressuring and depressurizing with nitrogen at 500 psi to 50 psi several times, while stirring.

[0037] 3. Under an initial nitrogen pressure of 500 psi, the mixture was heated slowly to 180° C. and kept at this temperature for over 14 hours. During the process, a maximum pressure of 740 psi at 180° C. was observed. Then, the pressure lowered with time due to the condensation of ethyl acetate from vapor phase into liquid phase.

[0038] 4. The lowering of pressure stopped after about 8 hours. The mixture was then cooled to ambient temperature, excessive gas was vented and the product was recovered as a light brown liquid. The crude product was rotovapped at 70° C. to remove ethyl acetate. 207 g of the crude product was obtained.

Example 2

[0039] Second Step: Butoxylation of DETA-Triamide

[0040] 1. A mixture of DETA-triamide (13.74 g, 0.06 moles), potassium hydroxide (0.27 g) and 1,2-epoxybutane (82.22 g, 1.11 moles) were charged into a one-liter autoclave.

[0041] 2. The autoclave was sealed and was purged off air by pressuring and depressurizing with nitrogen at 500 psi to 50 psi several times, while stirring.

[0042] 3. Under an initial nitrogen pressure of 500 psi, the mixture was heated slowly to 120° C. and kept at this temperature for over 17 hours. During the process, a maximum pressure of 639 psi at 120° C. was observed. Then, the pressure lowered with time due to the condensation of 1,2-epoxybutane from vapor phase into liquid phase.

[0043] 4. The lowering of pressure stopped after about 9 hours. The mixture was then cooled to ambient temperature, excessive gas was vented and the product was recovered as a light brown liquid. The crude product was rotovapped at 70° C. to remove 1,2-epoxybutane. 91.87 g of the crude product was obtained.

[0044] 5. The product was subjected to GPC, NMR and IR analyses after washing out K⁺ with distilled water. GPC analysis indicated an average molecular weight of Mw=1435.

Example 3

[0045] Selective Hydrolysis of the Butoxylation Product of Triamide with 10% HCl Solution

[0046] 1. A mixture of the butoxylation product of triamide (20 g) and 10% HCl solution (80 g) were charged into a beaker and mixed with a magnetic stirrer while refluxing at 90-100° C.

[0047] 2. During the reaction, small amount of samples was taken from the beaker and was subjected to IR analysis in order to monitor the reaction. After about 8 hours, disappearance of IR absorption peak characteristic of C═O (1735 cm⁻¹) indicates the completion of the reaction.

[0048] 3. Turn off the heater and stop the reaction. The mixture was then cooled to ambient temperature. A mixture of 40 ml pure water and 40 ml toluene was used to extract and dilute the acidity of the solution.

[0049] 4. 40 ml of 1 N NaOH was used to neutralize the toluene layer and the water layer was discarded.

[0050] 5. 40 ml of water was used to extract NaOH in the upper layer twice.

[0051] 6. The crude product was rotovapped at 70° C. to remove 1,2-epoxybutane. 12.5 g of the crude product was obtained. The yield was 60%. After washing out K+with distilled water, the product was subjected to GPC, NMR and IR analyses after washing out. GPC analysis indicated an average molecular weight of Mw=1375.

[0052] Test Results

[0053] In each of the following tests, the base fuel was an unleaded gasoline that contained no additive. The Gemini poly(oxyalkylene)diamide compounds utilized were prepared as indicated by Example number and were used at the concentration indicated in ppm by mg/ml. The test employed are described hereinafter and the results of the various tests are set forth in tables below. The following tests may also contain one or more additional detergents. When additional detergents are used, the fuel composition will comprise a mixture of a major amount of hydrocarbon in the boiling range as indicated, a minor amount of an additional detergents selected from polyalkenyl amine, poly(oxyalkylene) carbamates and mixture thereof. Since some benefits may be derived from using carrier fluid, some tests by incorporating 100 or 200 mg/l of polyether type carrier fluid were also evaluated.

[0054] Intake Valve Coking Simulator (IVCS) Test

[0055] The IVCS test is a measure of the deposit formation on the hot ramp, the results denotes the tendency of the additive package dispersing the carbonaceous deposit generated on the film. The deposit simulator results were shown to correlate with BMW intake-valve deposit test. The test fuel is pumped to an injector consisting of a water-cooled hypodermic needle. The ramp is heated at the elevated end with six electric heaters and thermally insulated to achieve a temperature difference of 400° C. at the elevated end and 120° C. at the bottom of the ramp. In the IVCS test equipment, four parallel test cells were provided, so that four different samples can be tested at the same time.

[0056] The properties of the base fuel are as follows: Property Value IBP  40.3° C. 50% BP 108.1° C. 90% BP 163.5° C. Aromatics 41.6 vol. % Olefins  2.8 vol. % Saturates 48.1 vol. % MTBE  7.5 vol. % RON 92

[0057] The test conditions are as follows: Test fuel volume: 250 ml Test fuel flow: 0.83 ml/min. Ramp slop: 5° Stainless steel film 47 mm W × 10110 mm L × 0.02 mm T

[0058] Before test, stainless steel films were thoroughly cleaned with solvent (50% n-hexane and 50% acetone), then put the films in an oven at a temperature of 120° C. for 1 hour to remove solvent and water. New test film were weighed and installed, tests were run for a period of about 5 hours. At the end of each test, the film was removed, cleaned and re-weighed. Weight gain of the deposit on the film is the IVCS index, reported in mg/250 ml. Generally, the less the deposit formed, the better the intake valve detergency performance of the gasoline or additive tested was. Experience has shown that gasoline giving deposit less than about 3.0 mg/250 ml provides good intake valve detergency performance. TABLE 1 Con- Additional Additional Deposit Compound centration detergent conc. carrier fluid mg/250 Example # mg/l mg/l conc. mg/l ml — 0 — 0 12.0 ± 0.3¹ — 0 — 200 6.5 2 200 — 0 15.8 2 200 — 200 2.9 3 200 — 0 20.5 3 200 — 200 5.0 3 100 100(GKA67²) 0 2.8 3 100  50(GKA67²) 200 3.4

[0059] Thermal Decomposition Test

[0060] In order to evaluate the CCD performance of the novel gasoline additive, thermal decomposition test was conducted under following test conditions and sequences: Test sample weight: 0.2 g Container: Ceramic crucible Size: 5 cm diameter, 0.5 cm depth Oven: Lindberg, Blue M-Model 848 Test condition: 300° C., 60 min.

[0061] The results of the thermal decomposition tests are set forth in table 2. TABLE 2 Residue Compound Concentration (wt. %) Example # (wt. %) 300° C., 60 min. 2 100 2.0 3 100 4.4 OGA480¹ 100 2.5 PEA-Texaco² 100 4.1 OGA472³ 100 42.4

[0062] It is well known that the fewer residues formed at 300° C., the better combustion chamber deposit control and low ORI value are. OGA-480 controls engine ORI whereas OGA-472 tends to cause engine ORI. From the above thermal data, Example 2 and 3 have nearly the same performance in CCD control better than OGA 480.

[0063] Method for Octane Requirement Reduction Test

[0064] The purpose of octane requirement reduction test is to provide a method of determining the effect of various gasoline components and additives upon the octane requirement of the engine.

[0065] The experiment rig consisted mainly of a single-cylinder Waukesha CFR (Cooperative Fuel Research) gasoline engine, a pressure transducer, a charge amplifier, and a FFT (Fast Fourier Transform) signal analyzer. The critical CFR engine parameter and engine operating conditions are shown as follows. Engine: Waukesha CFR engine 612 cc, single cylinder, carburator Air inlet temperature: 38° C. Compression ratio: 7.0 Test condidiotns: Air/fuel ratio: 13.5 Spark timing: 23 BTDC Cooling temperature: 100° C.

[0066] Before starting of octane requirement reduction (ORR) test, the CFR engine has been dirty up after running engine test of accumulating 200 hours. Then the initial octane requirement (ONR) of fuel for the CFR engine is determined by detecting knock. The primary reference fuels (PFR) of a variety of RON blended by isooctane and normal heptane are used as ONR rating fuels. If the light engine knock occurred, the FFT signal analyzer will display a signal whose amplitude is higher than −53 dBVr in spectrum correlated by ear rating. The knock signal of the CFR engine comes out around the frequency of 5.8-6.4 kHz. The criterion of determining the ONR value for the engine was determined on the 25 percentage of light knock occurring frequency of 100 consecutive power cycles obtained using an intrapolation method.

[0067] Then the 60-hour engine ORR test starts to run using base fuel prepared by blending gasoline with 200 mg/l of Example 2 and 3 additives. Properties of the base fuel are shown as follows. Property Value IBP  40.0° C. 50% BP 108.6° C. 90% BP 170.5° C. Aromatics 26.8 vol. % Olefins 25.1 vol. % Saturates 48.1 vol. % RON 95

[0068] During the test, the duration of rating interval for ONR is typically eight hours. When the engine test was completed, the final ONR was rated again. The total ORR was calculated as the difference between the ONR numbers of the engine at the beginning and the end of the engine test.

[0069] The ORR performances of two additives, Example 2 and 3, have been measured. At the beginning of ORR test, the initial ONR of the CFR engine is 90.5 RON. The test results for additives are shown in Table 3. It can be seen that example 2 shows no ORR performance. After completion of the ORR test for Example 2, the engine was dirty up using base fuel by 24 hours until the ONR condition became 90.7 RON. Then the ORR test for Example 3 was started. The ORR performance for additive Example 3 is 2.1 RON compared with Example 2 as shown in Table 3. TABLE 3 Run 1 Run 2 Base fuel + Example 2 Base fuel + Example 3 Test fuel (RON) (RON) 1. ONR at 0 hours 90.5 90.7 2. ONR at 30 hours 90.1 89.3 3. ONR at 60 hours 90.6 88.6 4. ORR = ONR@0 hrs − ONR@60 hrs

[0070] Many changes and modifications in the above described embodiment of the invention can, of course, be carried out without departing from the scope thereof. Accordingly, to promote the progress in science and the useful arts, the invention is disclosed and is intended to be limited only by the scope of the appended claims. 

What is claimed is:
 1. A process for manufacturing gasoline additives of Non-ester polyoxyalkylene amide, comprising: (1) taking acetate alkyl esters and selecting from polyethylene oxide ether amine and polypropylene oxide in high temperature convert amides by amidation; (2) taking 1,2-epoxybutane and said amides yielding poly(oxyalkylene)amide and by-product which being poly(1,2-epoxybutane) ether-amine-ether-amide by butoxylation; and (3) said poly(1,2-epoxybutane) ether-amine-ether-amide selective acid/base hydrolyzing poly(1,2-epoxybutane)amine-alcohol-amide and removing the acetic acid by-product by selective hydrolysis in sit.
 2. The process of claim 1 wherein major product have the following formula:


3. The process of claim 2 wherein said amine select from poly(ethylene oxide)aminde

poly(propylene oxide)amine and alkylamine.
 4. The process of claim 1 wherein said acid/base hydrolysis used HCl solution.
 5. The process of claim 4 wherein said acid/base hydrolysis used 8 to 12% HCl solution.
 6. The process of claim 4 wherein said acid/base hydrolysis used 10% HCl solution.
 7. The process of claimi 1 wherein said high temperature is between 120° C. and 250° C.
 8. The process of claim 1 wherein said high temperature is 180° C.
 9. The process of clami 1 wherein said by-product hydrolyzes have the following formula: 